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Definitions

• the present invention relates to the field of adsorption or absorbent masses and also that of the purification of gaseous and liquid effluents such as liquid hydrocarbon feedstocks, natural gases, synthesis gases containing, among other things, sulfur impurities such as H 2 S, COS, and / or CS 2 , or halogenated impurities such as 1 HCl.
• gaseous and liquid effluents such as liquid hydrocarbon feedstocks, natural gases, synthesis gases containing, among other things, sulfur impurities such as H 2 S, COS, and / or CS 2 , or halogenated impurities such as 1 HCl.
• gaseous and liquid effluents such as liquid hydrocarbon feedstocks, natural gases, synthesis gases containing, among other things, sulfur impurities such as H 2 S, COS, and / or CS 2 , or halogenated impurities such as 1 HCl.
• adsorption mass, adsorbent or solid are used to
• the subject of the invention is a process for the multi-stage preparation of a ZnO-based capture mass.
• the solid obtained is in the form of extruded particles containing at least ZnO and at least one binder. Thanks to the method of preparation according to the invention, the solids obtained have very good mechanical strength properties, adapted to implementation in a fixed bed, as well as improved sulfur and HCl absorption capacities.
• the synthesis gases can conventionally be obtained by transforming natural gas, coal, heavy petroleum residues or biomass by processes such as steam reforming, autothermal reforming, or partial oxidation, or by decomposition of methanol.
• the synthesis gases can also be obtained by gasification of mixtures of biomass and / or coal and / or petroleum residues (synthesis gas obtained by "co-processing" according to English terminology).
• the synthesis gases contain variable contents of impurities such as, for example, sulfur compounds such as I 1 H 2 S, COS and / or CS 2 , as well as halogens such as chlorine in HCl form.
• Impurities sulfur and I 1 HCl present in non-purified synthesis gas can lead to accelerated corrosion of the installations in which they are implemented, such as for example gas turbine in the gas cogeneration units synthesis and (IGCC or "Integrated Gasification Combined Cycle" according to the English terminology).
• the gases resulting from a cogeneration plant must also meet very specific specifications, related to the requirements of the processes placed downstream. Sulfur compounds as well as halogens are often encountered constituents which it is necessary to effectively remove. These impurities are also liable to poison the catalysts used for example in Fischer-Tropsch synthesis processes or in chemical synthesis processes such as methanol synthesis processes, or to reduce the performance of the materials used in the process. fuel cells.
• H 2 S present in natural gases is generally removed using Claus type processes.
• H 2 S contents generally remain in the natural gas, which can be significant depending on the intended application (reforming natural gas for the production of hydrogen or synthesis gas, for example).
• Liquid fillers such as hydrocarbons used for example as feedstock for catalytic reforming units, isomerization units, or hydrogenation units contain sulfur impurities such as I 1 H 2 S, as well as COS and CS 2 qu it is a matter of eliminating in order to protect the catalysts used in the units in which they are employed. Environmental constraints also impose the elimination of these impurities.
• L ⁇ C1 is also part of the impurities present in naphthas and gases from reforming units, sometimes up to 20 ppm by weight.
• solid such as an adsorbent or a capture mass
• the impurities to be removed interact chemically with the metal oxides contained in the capture mass to form a sulphide.
• the solids used as capture mass include, for example, oxides based on copper, zinc, magnesium, iron or manganese.
• Alumina and silica may be used as a carrier or binder.
• the patent FR 2 295 782 B1 relates to a solid mass that can be used for the absorption of hydrogen sulphide (H2S) and, if appropriate, of sulphide and carbon oxysulphide (CS2, COS), said mass containing from 20 to 85% by weight of zinc oxide, calculated as ZnO, from 0.9 to 50% of alumina, calculated as Al 2 O 3 , and from 2 to 45% of Group KA metal oxide, calculated as oxide. It is prepared by mixing a zinc compound, at least one aluminum compound and at least one HA group metal compound, preferably a calcium compound.
• the solid mass described in this patent has sufficient mechanical strength for ZnO contents of up to 80% by weight; beyond this content, the mechanical strength becomes too low and does not allow use in a fixed bed.
• US Pat. No. 4,071,609 describes a method for preparing a capture mass composed exclusively of ZnO.
• the particles constituting the mass are obtained by granulation from a powder of zinc oxide and water, without the addition of a binder, the granulation leading to the formation of ZnO agglomerates which are then converted into basic zinc carbonate. by treatment under flow of CO 2 .
• the carbonate thus formed is finally decomposed by a heat treatment under air, at a temperature of between 200 and 500 ° C., to lead to the formation of ZnO, the heat treatment making it possible to confer on the particles a specific surface area and an increased mechanical strength.
• patents FR 2,718,658 B1 and US 5,866,503 describe absorbent pellets comprising a mixture of a reactive metal oxide which may be zinc oxide, an inert metal oxide which is diluent, a high surface area silica and a binder.
• the zinc oxide content of the pellets is generally between 30% by weight and 60 or 65% by weight.
• these capture masses are used in the form of pellets at a minimum desulfurization temperature of 426 ° C for the French patent, and 315 ° C for the US patent.
• dehalogenation laminate of halogenated compounds
• conventionally capture masses such as dolomite-based solids, zeolites, basic or alkali-treated aluminas, or else zinc oxides may be used.
• treated aluminas for example with alkalis, alkaline earths, rare earths, and / or transition metals, is the most common for purifying gases.
• the preparation process according to the invention makes it possible to obtain ZnO-based solids that can be used for the desulfurization and / or the elimination of halogen compounds from gaseous and liquid feeds.
• the solids obtained according to said process have resistance properties mechanics, and this even in the case of solids for which the ZnO content is greater than 85% by weight.
• a single method of preparation can therefore be used regardless of the ZnO content, which makes it possible to obtain solids having a good mechanical strength and therefore usable in a fixed bed.
• the method according to the invention comprises at least the following steps: a) premixing the powders comprising at least one ZnO powder and at least one binder, for example in a mixer by rotating the mixer arms, b) mixing the a paste obtained by i. contacting the premixed powders, and a solution containing a peptizing agent, leading to the production of a paste (peptization), ii. kneading the dough, c) extruding the dough obtained in step b) at a pressure of between 3 and 10 MPa, d) drying the extrudates obtained in step c) at a temperature between 70 and
• Said process of preparation makes it possible to obtain solids having increased sulfur capacities, which can advantageously be used to desulphurize all gaseous or liquid feeds comprising 1 H 2 S. They also make it possible to eliminate the COS and / or the CS 2 possibly present.
• the solids obtained according to the process whose ZnO content is greater than 85% by weight are particularly suitable for this use.
• the solid obtained can be used to purify, for example, natural gases, synthesis gases used in chemical synthesis processes, Fischer-Tropsch synthesis processes, cogeneration units, as well as liquid hydrocarbons.
• the solid according to the invention has a high sulfurization capacity from 150 0 C, and thus makes it possible to purify a synthesis gas in a very thorough manner under advantageous conditions, because identical in terms of pressure, temperature and flow rate to those used in the Fischer-Tropsch unit downstream.
• the solid thus prepared can be optionally regenerated after use.
• the process according to the invention makes it possible to obtain solids having an improved ability to eliminate halogenated compounds (for example, dechlorination capacities) at low temperatures, that is to say from 20 ° C. , and thus make it possible to purify a gas or a liquid under conditions representative of a gas or a liquid at the outlet of a stabilizing column of a catalytic reformer.
• a solid having a ZnO content of between 30% by weight and 95% by weight, preferably between 40% by weight and 90% by weight can advantageously be used.
• the subject of the invention is a process for the preparation of a solid based on zinc oxide making it possible to eliminate sulfur and halogenated impurities from a gas, comprising the following steps: a) premixing of the powders comprising at least a ZnO powder and at least one binder, b) mixing a paste obtained by: i. contacting the premixed powders, and a solution containing a peptizing agent, leading to the production of a paste (peptization), ii.
• step c) extruding the dough obtained in step b) at a pressure of between 3 and 10 MPa, d) drying the extrudates obtained in step c) at a temperature between 70 and 160 ° C. over a period of time between 1 and 24 hours, e) calcination of extrudates dried at a temperature between 200 and 800 0 C for a period of between 1 and 6 hours under a gas stream comprising oxygen.
• Said solid based on zinc oxide is in the form of extruded particles comprising at least: - 30% by weight to 98% by weight, preferably 40% by weight to 97% by weight, more preferably
• the solids obtained have improved desulfurization performance vis-à-vis the treatment of gases and liquids containing compounds H 2 S, COS and CS 2 .
• said solids have a sulfur capacity before drilling, measured by a drilling test carried out with a gas composed of 0.9% of 2 S in hydrogen, at a temperature of 200 ° C., at atmospheric pressure, with an hourly space velocity of 2600 h -1 , greater than 0.06 gram of sulfur per gram of solid, or even 0.08 or 0.10 gram of sulfur per gram of solid, and advantageously greater than 0.12 gram of sulfur. sulfur per gram of solid.
• the solids prepared by means of the process according to the invention have improved elimination performance of the halogenated compounds, particularly as regards the treatment of gases and liquids containing hydrogen chloride or hydrochloric acid (HCl ).
• said solids have a chlorine capacity, also measured by a drilling test with a gas composed of 500 ppm volume of H 2 O and of 500 ppm volume of HCl in nitrogen, at a temperature of 30 ° C.
• the ZnO content of said solid is preferably between 60% by weight and 95% by weight, and very preferably between 85% by weight and 95% weight of ZnO,
• the ZnO content of said solid is preferably between 30% by weight and 98% by weight, more preferably between 40% by weight and 80% by weight. % by weight, more preferably between 50% by weight and 70% by weight of ZnO.
• ZnO sources are generally derived from two major industrial processes. manufacture of zinc oxide: the indirect process or French process and the direct or American process.
• the French method consists, at the base, in heating the zinc near its boiling point.
• the vapors thus generated are oxidized by combustion in the air.
• the zinc flower is sucked by fans and sent to large rooms where particles are classified through partitions according to their size. This process leads to products of very high purity whose quality depends only on the initial purity of the metal.
• the origin of the direct process dates back to 1852 (The New Jersey Zinc Company).
• the raw material is zinc ore, ie often sulphides, carbonates or zinc silicates.
• This ore, mixed with charcoal is charged into an oven where a current of air circulates.
• the heat from burning coal allows the reduction of the ore and the volatilization of the zinc.
• These vapors are then oxidized by carbon dioxide or excess oxygen.
• the oxide fumes are sucked and driven in large spaces to recover particles classified by size. Although more economical, this process leads to a less pure zinc oxide.
• the zinc oxide powders used for the manufacture of the solid according to the invention usually have a specific surface (determined by adsorption-desorption of nitrogen) of between 10 and 80 m 2 / g approximately, most often between 30 and 60 m 2 / g.
• the ZnO powder is associated with at least one binder in order to allow the shaping of said solid and to give it good mechanical strength.
• the proportion of binder used during manufacture is less than or equal to 60% by weight (expressed on the basis of the total dry matter), and depends on the targeted application, preferably less than or equal to 5% by weight.
• the binder content of the particles is preferably between 1% by weight and 15% by weight.
• the binder content of the particles is preferably between 20 and 60% by weight and even more preferably it is between 30 and 50% by weight. .
• the solid according to the invention comprises at least one binder.
• Binders well known to those skilled in the art can be used; advantageously, for example, chosen from an alumina or an alumina precursor, which is preferably boehmite, silica, or a clay such as, for example, a kaolinite, a montmorillonite, a bentonite or a smectite. It is quite possible to combine an "alumina" type binder and a "clay” type binder.
• the binder is a kaolinite type clay, eg Provins clay.
• the solid prepared by means of the process according to the invention is obtained by bringing into contact at least one ZnO powder, a binder and a solution containing a peptizing agent according to a particular process.
• the invention therefore relates to a process for preparing a solid comprising ZnO and a binder, wherein said process comprises the following steps: a) premixing the powders comprising at least one ZnO powder and at least one binder, b) mixing a paste obtained by: i. contacting the premixed powders, and a solution containing a peptizing agent, leading to the production of a paste (peptization), ii. kneading the dough, c) extruding the dough obtained in step b) at a pressure of between 3 and 10 MPa, d) drying the extrudates obtained in step b) at a temperature between 70 and 160 ° C. over a period of time between 1 and 24 hours, e) calcination of the extruded dried at a temperature between 200 and 800 0 C for a period of between 1 and 6 hours, under a gas stream comprising oxygen.
• step a Description of step a:
• Stage a consists of a mixture of the powders, preferably dry, for example in a kneader or in any other type of mixer. This step, preferably carried out without addition of liquid, allows to obtain a homogeneous mixture of the powdery constituents.
• step b Description of step b:
• Step b consists in bringing the pre-mixed powders into contact during step a with a solution containing a peptizing agent.
• This step which makes it possible to obtain a paste, is intended to peptize the constituents.
• Step b which comprises a peptization, may be implemented according to two variants of the present invention, which differ in the constitution of the solution implemented in said step.
• the peptization is advantageously carried out using a solution containing a basic peptizing agent in order to allow:
• this first variant is operated in the absence of dopant.
• Dopant means a mineral element capable of being adsorbed on the surface of the ZnO particles and / or of being incorporated in the crystalline structure of ZnO.
• the use of a basic peptizing agent in the preparation of ZnO-containing solids used for the desulfurization of gaseous or liquid feeds is particularly advantageous. Indeed, it has been found that the use of a basic peptising agent for the preparation of solid according to this application makes it possible to achieve a substantial increase in the sulfur capacities of the solids used for desulphurization, relative to the solids of the solids. prior art.
• the peptization according to the first variant is carried out using a basic aqueous solution containing an inorganic base such as sodium hydroxide, potassium hydroxide, aqueous ammonia, or else at the same time.
• the inorganic base is sodium hydroxide.
• the pH of the solution used is greater than 8, preferably 10, more preferably greater than 12.
• These pH values are generally obtained by taking into account a base amount ratio. amount of ZnO between 1 and 10% by weight, preferably between 2 and 8% by weight.
• the peptization is advantageously carried out using a solution containing an acidic or basic peptizing agent and at least one dopant.
• Dopant means a mineral element capable of being adsorbed on the surface of the ZnO particles and / or of being incorporated in the crystalline structure of ZnO.
• the dopants may be for example alkaline or alkaline earth ions, or belong to the series of transition metals.
• the dopant is an alkaline or alkaline earth ion and very preferably the dopant is the sodium ion Na + .
• the peptization is advantageously implemented in order to allow:
• the peptization is preferably carried out with the aid of an aqueous solution containing, together with a peptizing agent and a compound containing a doping mineral element, or with the aid of a compound having the double doping / peptizing effect.
• the soda acts, by its composition, both as a peptizing agent and as a dopant since the Na + element is then provided by the sodium peptizing agent in the system. The same is true for mineral bases that allow the same effects.
• the doping mineral element is generally introduced into the aqueous solution used for the dispersion and peptization of the constituents ZnO and binder (s) during mixing.
• the content of doping mineral element introduced into the final particles is generally between 0.1 and 10% by weight, based on the dry mass of ZnO used, preferably between 0.5 and 6% by weight.
• the peptization of the ZnO and binder constituents may be carried out in acidic medium, the acid being most often nitric acid but may also be hydrochloric acid or any other known acid.
• an inorganic acid such as hydrofluoric acid, hydrobromic acid, hydrochloric acid, nitric, nitrous, sulfonic, sulfuric or perchloric acid, or else a mono or di- carboxylic acid such as acetic, propionic or butanoic acid.
• the peptization may also be carried out in a basic medium, using a solution containing an inorganic base such as sodium hydroxide, potassium hydroxide or ammonia, or else using a solution containing an organic base such as an amine, a quaternary ammonium compound, chosen, for example, from alkyl-ethanol amines or ethoxylated alkylamines.
• a solution containing an inorganic base such as sodium hydroxide, potassium hydroxide or ammonia
• an organic base such as an amine, a quaternary ammonium compound, chosen, for example, from alkyl-ethanol amines or ethoxylated alkylamines.
• the peptization is carried out using an acidic aqueous solution containing nitric acid.
• the pH of the solution (measured at ambient temperature) is preferably less than 5, preferably less than 3.
• These pH values are generally obtained by taking into account an amount ratio HNO 3 / amount of ZnO between 1 and 10% by weight. preferably between 2 and 6%.
• the peptization is carried out using a basic aqueous solution.
• the pH of the solution (measured at room temperature) is greater than 8, preferably 10, more preferably greater than 12.
• pH values are generally obtained by taking into account an amount of base / amount of ZnO ratio between 1 and 8% by weight, preferably between 2 and 8% by weight.
• the amount of liquid solution used is adjusted so as to obtain, at the end of the peptization and regardless of the variant used, a paste that does not run but is not too dry to allow extrusion in step c under suitable pressure conditions well known to those skilled in the art and dependent on the extrusion equipment used.
• the extrusion pressure is greater than 1 MPa, and preferably between 3 MPa and 10 MPa.
• the contacting of the reagents is carried out by kneading, batchwise or continuously.
• the powders (ZnO and binder) are first premixed before the introduction of the aqueous solution containing the basic peptizing agent. Whether for zinc oxide or the binder, it is quite possible to proceed with mixtures of several sources of ZnO and / or alumina or clay type binder.
• extrusion aids may for example be chosen from mono-carboxylic aliphatic acids, alkylated aromatic compounds, sulphonic acid salts, fatty acids, polyvinyl pyridine, polyvinyl alcohol, methylcellulose.
• These adjuvants are generally added at a content of between 1 and 20% by weight, preferably between 2 and 10% by weight, based on the total weight of the constituents introduced into the kneader.
• the mixing time is generally between 5 and 60 min, preferably between 20 and 50 min.
• the speed of rotation of the mixer arms is between 10 and 75 rpm, preferably between 25 and 50 rpm.
• the dough is extruded, for example into a piston, single-screw or twin-screw extruder.
• the mixing can be coupled with the extrusion in the same equipment.
• the extrusion of the kneaded dough can be carried out either by directly extruding the end of continuous twin-screw kneader for example, or by connecting one or more batch kneaders to an extruder.
• the geometry of the die which confers their shape to the extradited, can be chosen from the well-known sectors of the art. They can thus be, for example, cylindrical, trilobal, quadrilobed, fluted or slotted.
• step d Description of step d:
• the extrudates obtained are then dried at a temperature generally of between 70 and 160 ° C. for a duration of between 1 and 24 hours.
• the drying can be advantageously carried out in air or preferably in moist air.
• the extrudates obtained are then treated under a gaseous flow comprising oxygen, for example preferably calcined under air, or else treated in temperature in the presence of a gaseous mixture comprising an inert gas (for example nitrogen) and oxygen.
• a gaseous mixture comprising an inert gas (for example nitrogen) and oxygen.
• the gaseous mixture used preferably comprises at least 5% by volume, and preferably at least 10% by volume of oxygen.
• the temperature of said treatment is generally between 200 and 800 0 C, preferably between 300 and 600 0 C for a period of between 1 and 6 hours, preferably between 2 and 4 hours.
• the extrudates At the end of the calcination, the extrudates have a diameter of between 1 and 5 mm, preferably between 1.5 and 3.5 mm.
• the shape of the particles is similar to that of a cylindrical rod but it is not excluded that the particles are then, for example introduced into equipment to round their surface, such as a bezel or other equipment allowing their spheronization.
• this is determined by the grain-to-grain crushing test described by ASTM method D 4179-88a. This consists in measuring the breaking force of each particle of a representative sample comprising at least 50 particles. The result is weighted by the length of the extradite.
• the EGG value is the average of the breaking forces measured and reduced to the unit length of the extrudate (expressed in daN.mm- 1 ) for all the particles of the sample.
• the value of EGG is greater than 0.9 daN.mm- 1 (decaNewton per millimeter of extrudate length), preferably greater than 1.0 daN.mm " '.
• the sulfur capacity of the solid according to the invention is measured by a drilling test whose conditions are described below.
• the test is carried out at a temperature of 200 ° C., at atmospheric pressure, and with a hourly volume velocity (WH) of 2600 h -1 .
• the gas used for the test contains 0.9% H 2 S and 50 ppm.
• the contents of H 2 S and COS present in the gas leaving the reactor, which contains the capture mass used for the test, are determined by gas chromatography.
• the sulfur capacity of the solids according to the invention is determined by performing a material balance.
• the sulfurization capacity corresponds to the amount of sulfur accumulated by the solid before drilling (that is to say at the time t p shown in Figure 1 commented below), this being calculated using the following relation: with: q s : the mass of sulfur captured by the solid (in g),
• t p is the time to drill and fi t the time to end drilling.
• the sulfur capacity of the test solid is given by the relationship: ## EQU1 ## with the mass of absorbent used during the test.
• the chlorination capacity of the mass according to the invention is measured by a drilling test whose conditions are described below. The test is carried out at a temperature of 30 ° C., at atmospheric pressure, and with a hourly volume velocity (WH) of 1600 h -1 .
• the gas used for the test is composed of 500 ppm UH 2 O and 500 ppm. HCl in nitrogen
• the content of HCl present in the gas leaving the reactor, which contains the capture mass used for the test, is determined by NaOH titrimetry
• the chlorination capacity of the capture masses according to the invention is determined by performing a material balance
• the chlorination capacity, as defined according to the present invention corresponds to the amount of chlorine accumulated by the solid after drilling (that is to say at the time tf of FIG. ), this being determined by calculation of the amount of HCl reacted with NaOH as well as by analysis of the solid after reaction.
• the subject of the invention is also the use of the solid as described above with regard to its composition and method of production.
• the solid prepared by means of the process according to the invention can be used to purify any gaseous or liquid charge containing, inter alia, sulfur compounds such as H 2 S, COS and / or CS 2 . Said solid can also be used to remove 1 ⁇ C1 present in liquid or gaseous effluents.
• the solid is used by contacting the gaseous feedstock to be treated with said mass in a reactor, which can be either a fixed bed reactor, a radial reactor, or a fluidized bed reactor.
• the conditions of use of said solid are preferably such that the pressure is between 0.1 and 25 MPa, preferably between 0.1 and 15 MPa, and the temperature of between 100 and 450 ° C.
• the solid prepared according to the invention can be used to purify gaseous feeds such as, for example, those used in cogeneration plants, in chemical synthesis units such as methanol synthesis units, or liquids such as hydrocarbons used as fillers in catalytic reforming, isomerization, or hydrogenation units.
• the synthesis gas is generally used at a pressure of between 1 and 10 MPa, and at a temperature of between 100 and 280 ° C.
• the synthesis of methanol is generally carried out in the most recent processes under a pressure of between 1 and 15 MPa, preferably between 5 and 10 MPa and at a temperature of between 150 and 300 ° C., preferably between 220 and 300 ° C. and 280 ° C.
• the solid prepared according to the invention can be advantageously used to purify the feedstock of a Fischer-Tropsch synthesis unit, by using it in a reactor operating at a pressure generally of between 0.1 and 15 MPa. preferably between 1.5 and 5.0 MPa, at a temperature most often between 150 and 400 0 C, preferably between 170 and 350 0 C.
• the conditions of use of said solid are preferably such that the pressure is between 0.1 and 10. MPa, preferably between 1 and 5 MPa, and the temperature between 20 and 190 ° C.
• the invention therefore also relates to the use of the solid prepared by means of the preparation method according to the invention, for desulfurizing a gas or a liquid, at a temperature of between 100 and 450 ° C. and a pressure of between 0.1 and 25 MPa.
• It also relates to the use of the solid prepared by means of the preparation process according to the invention, for eliminating halogenated compounds from a gaseous or liquid charge, at a temperature of between 20 and 190 ° C., and a pressure of between 0.1 and 10 MPa.
• the capture masses referenced 1 and 2 are prepared by kneading-extrusion, according to the following procedure: a) premixing the powders comprising the ZnO powder and the binder in a kneader by rotating the arms of said kneader. b) kneading of the dough obtained by iii. contacting the premixed powders, and the solution containing nitric acid, leading to obtaining a paste (peptization). iv.
• the capture mass 3 is prepared according to the following procedure: b) mixing step in which the ZnO and binder powders are simultaneously brought into contact by gradually introducing them into the nitric acid solution and then kneading together until one of a paste (peptisation) is obtained.
• the formulation of the solids is given in Tables 1 and 2.
• the ZnO content is 70 or 95% by weight depending on the solids.
• the amount of HNO 3 acid is 2% by weight based on the amount of ZnO introduced.
• This example shows the characteristics and performance of solids 1 and 2, for which a commercial ZnO is used, the binder being a commercial boehmite.
• the ZnO mass contents of solids 1 and 2 are 70 and 95% by weight, respectively, and the boehmite binder contents, respectively, of 30 and 5% by weight.
• the pressure varies between 7.7 and 9.4 MPa for the solid 1.
• the pressure varies between 3.5 and 5.4 MPa for the solid 2.
• the extrudates are calcined for 2 hours at 650 ° C.
• the increase in the ZnO content leads to an increase in the sulfur absorption capacity, but also induces a deterioration of the mechanical strength properties of the capture masses according to this procedure.
• the mechanical strength of the solid 2 is too low given the constraints related to industrial use, and moreover the sulfur absorption capacity remains poor despite the high content of ZnO.
• This example shows the characteristics and performance of the solid 3, for which a commercial ZnO is used, and the binder is a kaolinite type clay.
• the ZnO and clay mass contents of the solid 3 are respectively 95 and 5% by weight.
• the sulfur capacity of the solid remains a low level compared to that of the solids according to the invention.
• step b) extrusion of the paste obtained in step b) with the aid of a piston extruder made of cylinders with a diameter of 3 mm, and with a length of 5 to 10 mm at a pressure varying according to the solids.
• the formulation of solids 4 to 8 corresponds to 95% by weight of ZnO and 5% by weight of binder.
• the solid 9 is prepared according to the same procedure, the amount of ZnO used being
• the mechanical strength of the extrudates is determined by a mechanical test of grain-to-grain crushing type as described above.
• This example shows the properties of solid 4, for which the same commercial ZnO used in the preceding examples is used, and the binder is a commercial boehmite.
• the peptization is carried out using a NaOH sodium hydroxide solution, the base NaOH content expressed relative to the mass of ZnO introduced is set at 2% by weight. As a result, the mass content of sodium ion
• Na + is 1.2% relative to the amount of ZnO introduced.
• the extrusion pressure is between 5.0 and 8.0 MPa.
• Extrudates are calcined for 2 hours at 650 ° C.
• This example shows the properties of the solid 5, for which a commercial ZnO is used, and the binder is a kaolinite type clay.
• the peptisation is carried out using a NaOH sodium hydroxide solution, the base NaOH level expressed relative to the mass of ZnO introduced is fixed at 4% by weight. As a result, the mass content of sodium ion
• Na + is 2.4% relative to the amount of ZnO introduced.
• the pressure varies between 5.0 and 8.0 MPa.
• This example shows the properties of the solid 6, for which a commercial ZnO is used, and the binder is a boehmite.
• the peptisation is carried out using a NaOH sodium hydroxide solution, the base NaOH level expressed relative to the mass of ZnO introduced is fixed at 4% by weight. As a result, the mass content of sodium ion
• Na + is 2.4% relative to the amount of ZnO introduced.
• the pressure varies between 5.3 and 6.5 MPa.
• the extrudates are calcined for 2 hours at 500 ° C.
• This example shows the properties of the solid 7, for which a commercial ZnO is used, and the binder is a kaolinite type clay.
• the peptization is carried out using a basic solution of ammonia, the base NH 4 OH level expressed relative to the mass of introduced ZnO is fixed at 2% by weight
• the pressure varies between 6.0 and 7.5 MPa.
• This example shows the properties of the solid 8, for which a commercial ZnO is used, and the binder is a kaolinite type clay.
• the peptization is carried out using an acidic solution of HNO 3 additive of sodium nitrate.
• the amount of HNO 3 is 3% by weight relative to the amount of ZnO introduced.
• the dopant is the sodium ion Na + , the content introduced during the peptization is 2% by weight relative to the dry mass of ZnO.
• the pressure varies between 4.5 and 7.0 MPa.
• the extrudates are calcined for 2 hours at 500 ° C.
• This example shows the properties of the solid 9 for which a commercial ZnO is used, and two boehmite and clay binders have been used.
• the amount of boehmite used for the shaping of the solid is here 39% by weight relative to the total mass of the sample, and the content of clay kaolinite type is 3% by weight.
• the peptization is carried out using a nitric acid solution, the level of HNO 3 acid expressed relative to the mass of ZnO introduced is fixed at 1.3% by weight.
• the Na + sodium level introduced during the peptization is 0.1% relative to the mass of ZnO introduced.
• the pressure varies between 6.0 and 7.5 MPa.
• the extrudates are calcined for 2 hours at 700 ° C.
• the chlorine capacity of the solid 9 is particularly high, being equal to 0.26 gCl / solid, which corresponds to a specific capacity of 26% under the conditions of the drilling test.

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